ANALYSIS REPORT 


ON THE 

Granger Water Gas 

/ 

- BY 

Dr. GIDEON E. MOORE, 

Analytical Chemist, 

NEW YORK. 


TOGETHER WITH A BRIEF 

DESCRIPTION OF THE PROCESS AND 
APPARATUS. 


A. O. GRANGER & CO., 

22 and 24 N. Fourth St., and 400, 402 and 404 Commerce St., 
PHILADELPHIA. 

1885. 









ANALYSIS REPORT 


ON THE 



BY 

Dr. GIDEON E. MOORE, 

o 

Analytical Chemist, 

NEW YORK. 


TOGETHER WITH A BRIEF 

DESCRIPTION OF THE PROCESS AND 



22 and 24 N. Fourth St., and 400, 402 and 404 Commerce St., 
PHILADELPHIA. 

1885. 





Copyright 1885, 

BY 

A. O. Granger & Co. 


Edward Patteson, Printer, 18 South Third St., Philadelphia. 

A 


Y(<L CJLZj V "(Ml 


bo 

c 


iii 


INDEX. 


DESCRIPTION OF THE WORKS AND 

METHOD OF OPERATING,. 7 

Chief point of superiority,. 13 

Cost of the Gas,.15 


REPORT OF Dr. GIDEON E. MOORE, . 17 

Principle upon which the Granger system is 

based, ..18 

Method of analyses and apparatus employed, . 19 

I. COMPOSITION OF THE GAS,.20 

Preliminary analysis of non-luminous Gas at 

Worcester,. 21 

Preliminary analysis of Holder Gas, Worcester 

and Lake,. 22 

Determination of character of Heavy 

Hydro-Carbons,. 23 

1st. Examination of Tar,.24 

2d. Examination of products obtained by action 

of Bromine on Water Gas,.24 

3d. Examination of products obtained by solu¬ 
tion in absolute Alcohol,.26 

Results of above determination,. 26 















IV 


Quantitative proportions of illuminat¬ 
ing Hydro-Carbons in Gas from con¬ 
denser at Lake,. 27 

A. Preliminary analysis,.27 

B. Eudometric analysis,. 28 

C. Complete analysis,.29 

Complete analysis of Holder Gas at Worcester 

and Lake,.29 

Analysis of Coal Gas for comparison with above, 30 

II. CALORIFIC VALUE OF THE GAS, ... 31 

Calorific equivalent. Definition of the 

term,. 31 

Method of determination,.32 

Table of Calorific Equivalents of Constituents 

of Illuminating Gas,.33 

Calorific Equivalent of Granger Gas at Wor¬ 
cester, .33 

Calorific Equivalent of Granger Gas at Lake, . 35 
Calorific Equivalent of Coal Gas at Heidelberg, 36 

Results compared,. 37 

Flame-Temperature. Definition of the 

Term,.37 

Manner of investigating,. 39 

Flame-Temperature of Granger Gas at Wor¬ 
cester, .40 

Flame-Temperature of Granger Gas at Lake, . 41 
Flame-Temperature of Coal Gas at Heidelberg, 43 
Comparison of results,. 44 

III. PHOTOMETRY OF THE GAS,.45 

Candle power of the Gas at Worcester, .... 46 

Candle power of the Gas at Lake,. 46 

Candle power regulated at will,.46 

















V 


/ 

Quality of the light,. 46 

Influence of extreme Cold on Illumi¬ 
nating Power, . 46 

Freezing test, Granger Gas at Worcester, ... 48 
Freezing test, Coal Gas at Worcester, .... 48 

Reasons why Water Gas should resist cold better 

than Coal Gas,. 49 

Relations of Chemical Composition to 
Illuminating Power, ..49 

IV. DENSITY OF THE GAS,. 55 

Water Gas at Worcester,.55 

Water Gas at Lake,. 55 

Coal Gas at Heidelberg,.55 

V. PURITY OF THE GAS, . 56 

Quantitative determination of impurities, . . 56 

The Granger Gas of the highest degree of purity, 57 

VI. SUMMARY OF RESULTS,. 57 

Uniformity in composition as compared with 

Coal Gas,.58 

It will not stratify in the Holder, . 59 

Distinctive feature of the Granger process, . . 6o 
Table II. Results of analysis of Granger Gas at 
Worcester and Lake, and of Coal Gas at 

Heidelberg,.63 

Table I. Analyses of the Coal Gas of 27 
English and Scotch companies, .... 64-65 
















T HE cut at the back of this pamphlet 
gives a very fair idea of the appearance 
of our improved Water Gas apparatus, and the 
following brief description of the method of 
operating the works is given to make clear the 
subject in connection with Dr. Moore’s report 
on the Analysis of the Gas. 

A fire of anthracite coal or coke being started 
in Generator A, an air blast from the Blower B 
is admitted below the grate bars of the Gene¬ 
rator, by opening the valve C, and the pro¬ 
ducts of partial combustion, (Carbonic Oxide 
and Nitrogen) pass to the Superheater D 


How the 
works are 
operated. 


Blowing up 
the heat. 


8 


Ready to 
make Gas. 


Steam 
turned on. 


through the flue E, and meet another blast of 
air by opening the valve F. Complete com¬ 
bustion takes place, and the heat evolved is 
absorbed by the fire brick with which the 
Superheater D is filled, and the products of 
complete combustion (Carbonic Acid and Ni¬ 
trogen) pass off to the open air through the 
Stack-valve G. 

When the Superheater is hot enough, which 
can be seen by looking through the sight cock 
H, the air valves F and C are closed, and the 
lever I is pulled downwards, with the simulta¬ 
neous effect of closing the stack-valve G, at 
top of Superheater, and removing to the left 
the hood seal J, thus uncovering the upper 
end of the gas pipe K, which extends into the 
seal chamber Y. 

Steam is now admitted under the grate bars 
of the Generator, by turning the index lever 
L, which controls the steam valve below. The 
steam in passing through the bed of coal is 
decomposed, forming Hydrogen and Carbonic 
Oxide, which gases burn with great heat, but 
no luminosity. 


9 


Naphtha or crude petroleum is now sprayed Oil admitted, 
in the form of a mist into the base of the 
Superheater D, through the spraying injector 

M, being first forced through the oil heater 

N, by the plunger steam pump O. A very 
thorough incorporation of the particles of oil 
with the hot Water Gas, as it comes through 
the flue E, takes place and the oil in this finely 
divided state is vaporized by the heat of the 
Gas from the Generator, and the mixture 
passes upwards through the hot fire brick 
in the Superheater D, with the result of pro¬ 
ducing a perfectly fixed Illuminating Gas, 
which passes off through the pipe P, into 
the seal chamber Y, and downwards from it 
through the pipe K into the Scrubber Q, where 
it passes through wrought iron perforated 
plates, placed both vertically and at an angle, 
over which warm water from the Condenser 
flows, and is thus thoroughly scrubbed. The 
Gas then passes through the pipe R, to the 
Condenser, and downwards through the tubes 
S, which are surrounded with water, and off to 
the lime purifiers through the exit pipe T. 


IO 


Time blow¬ 
ing and 
making Gas. 


Short runs 
the best. 


Checker 
brick work 
condemned. 


The process of blowing up the heat takes 
from six to tfen minutes, and the time of 
making a run of Gas, i. e., with steam and oil 
on, from ten to fifteen minutes. The process 
is thus an alternate one, although several runs 
are made from one coaling of the Generator. 

We prefer short runs, and make our bed 
of Coal in the Generator of large area and 
shallow depth to accomplish this purpose, as 
we thus make all our Gas at high heats, and 
avoid the deleterious products resulting from 
long runs and low heats. 

The usual practice is to fill the Superheater 
or fixing chamber D, with checker brick work, 
but experience shows that the flat surfaces pre¬ 
sented by each layer of bricks afford a lodging 
place for cinders, etc., coming from the Gen¬ 
erator, and these cinders are soon burned into 
a slag, and in a short time the Superheater is 
clogged up and the bricks require to be taken 
out and others put in their places, and this is 
often a difficult job, as the bricks, cinders, 
etc., are found run together in a solid mass. 


II 


Our form of fire brick filling is that of a cyl¬ 
inder about 6 inches high, with a conical hole 
through it, larger at the upper end than at the 
lower. These bricks are placed one on top of 
the other, as shown in the cut, forming a series 
of straight holes from top to bottom, and yet 
the Gas in passing through these bricks, by 
reason of the conical shape of the interior 
hole, is given a whirling or eddying motion, 
thus bringing it into contact with the hot sur¬ 
faces and perfectly fixing the Gas and yet pre¬ 
serving a straight hole from top to bottom, 
and offering no flat surface anywhere for the 
lodgment of cinders or other matter mechanic¬ 
ally suspended in the Gas. While being in 
every way as effective as the old form, we claim 
that our conical bricks will last many years 
longer than the best form of checker brick 
work ever devised. 

We call attention to our Seal Chamber Y, 
in which the Hood Seal J effectually seals the 
pipe K, while blowing up the ’heat, and when 
making Gas permits the Gas to pass to tne 
Scrubber without being forced through a body 


Improved 
conical fill¬ 
ing bricks 
for Super¬ 
heater. 


Improved 
open seal. 


12 


Piping of 
Condensers. 


Shaking 
Grate for 
Generator. 


of water, which latter is the cause of produc¬ 
ing considerable tar, and also of increasing the 
back pressure on the works, and of causing the 
Gas to be delivered in a pulsating movement 
with the effect of blowing out the seals in vari¬ 
ous parts of the works. Our Gas is delivered 
at a nearly uniform pressure, and entirely 
avoids these objectionable features. 

Cold water is admitted to the bottom of the 
Condenser, and the warm water overflows from 
the top to the Scrubber and Seal Chamber; 
the Gas thus comes in contact first with the 
warmest part of the Condenser, and leaves it 
at the coolest part, and no matter how many 
Condensers are used, we pipe them in the 
same way, so that there is a gradual and uni¬ 
form reduction of the temperature of the Gas. 

The Pressure Gauges X give a convenient 
index of the pressure in various parts of the 
works. 

We have a very complete shaking grate 
operated from the working floor by the lever 
U, and the ashes fall into the inverted conical 
bottom V, where they may be allowed to col- 


x 3 

lect, and only require dumping once or twice 
a day, when the lid W is opened by operating 
a convenient lever and the ashes dropped into 
the buggy, where they are sprinkled with 
water and removed with but little of the or¬ 
dinary labor and dirt attendant upon cleaning 
a Generator fire. 

While making strong claims as to the con¬ 
venience in operating our works, and their 
mechanical appearance and durability, yet we 
have also studied simplicity, and on this im¬ 
portant point claim to be without any rival. 

That our Gas is perfectly fixed, and has 
ability to resist cold without condensing, far 
in excess of that of the best Coal Gas, is 
clearly shown by the freezing tests to which 
the Gas was submitted by Dr. Moore, as de¬ 
tailed on pages 46, 47 and 48. 

The main point upon which we base our 
claim of superiority, is our method of Carbu- 
retting the Gas. Where the Oil is allowed to 
run in as a liquid on top of the bed of Coal, 
it is apparent that, if the Coal is too hot, lamp 
black will be the immediate result, and if it is 


Simplicity. 


Fixed Gas. 


Superiority 
of Spraying 
the Oil. 


14 


not hot enough, the Oil will not only not be 
vaporized, but will actually run through the 
fire, and be found as free Oil in the ash pit, 
and will produce considerable tar. In either 
case, a loss of material is the result, besides 
annoying stoppages in the works. We spray 
the hot Oil through the Injector M in the form 
of a very fine mist, right into the hot Water 
Gas, as it issues from the Generator through 
the flue E, and it is completely vaporized by 
the heat of the Gas, without the formation of 
either lamp black or tar, and we can produce 
the maximum result, no matter whether the 
top of the bed of Coal in the Generator be 
perfectly black, or at an intense white heat. We 
thus utilize all the Oil, and attain the highest 
degree of economy, and the candle power of 
the Gas is under perfect control of the Gas 
maker, so that anything from a blue light to 
30 candle power, can easily be produced at 
will. 

We have many minor improvements of value 
that have suggested themselves in the course of 
long years of experience, gained in building 


*5 

over 70 sets of Water Gas works, and we 
may add that, in our largest size works, 
we can produce 18 to 20 candle power Gas 
from 45 lbs. of Coal and 3.75 galls, naphtha 
per thousand feet, and over 100,000 feet per 
day per man. 

We believe in Water Gas on its merits , and 
solicit correspondence. 

A. O. GRANGER & CO., Engineers, 
Patentees and Builders, 

22 and 24 North Fourth St., 
Philadelphia, Pa. 

A. O. GRANGER. JOS. H. COLLINS, JR. 


Cost of the 
Gas. 
















i7 


Analytical Laboratory of 
Dr. Gideon E. Moore, 

69 Liberty Street, 
New York, June 20th, 1885. 


Messrs. A. O. Granger & Co., 

Engineers and Contractors , 

22 and 24 North Fourth St., 

Philadelphia. 


Gentlemen : 


I have the honor to submit the 
following report of the results of my analyses 
of the Gas made in your Water Gas apparatus 
at the works at Lake (Chicago), Ill., and Wor¬ 
cester, Mass. 

Permit me, in this place, to express my 
grateful appreciation of the unvarying kindness 
and courtesy with which Mr. J. H. Rollins, 
Agent of the Worcester Co., and Mr. H. D. 
Bannister, Superintendent of the Lake Co., 
have extended every assistance and facility in 
their power during the progress of the work. 

Very respectfully, 

Gideon E. Moore, Ph. D. 


18 


REPORT. 

The principle upon which the Granger sys¬ 
tem of manufacture of Illuminating Water Gas 
is based consists, first, in generating ordinary 
“WaterGas” bypassing steam through incan¬ 
descent anthracite coal or coke, then diffusing 
through the hot Gas as it issues from the Gen¬ 
erator petroleum naphtha or other hydro-carbon 
substances by spraying them under mechanical 
pressure, and finally causing the mixture to 
pass through a Superheater previously heated 
to redness, wherein by the heat of the incan¬ 
descent fire-brick work, with which the Super¬ 
heater is filled, the hydro-carbon vapors are 
converted into permanent Gases and the trans¬ 
formation of the Water Gas into Illuminating 
Gas is completed. From the Superheater the 
Gas then passes through the Scrubber where it 
is washed with a spray of warm water, and 
then through the Condenser, wherein the Gas 
is cooled and any liquid or solid impurities that 
it may contain are removed ; finally it passes 
through the lime purifiers, wherein the purifi- 


*9 


cation is completed and the Gas made ready 
for delivery into the holder and for distribution. 

The material for the following analyses was 
collected by myself at the works at Lake, Cook 
Co., Ill., and at Worcester, Mass. At the 
Lake works the older form of the Granger plant 
was in use. In this case the hydro-carbon 
(naphtha at 72 0 Be) was sprayed under me¬ 
chanical pressure into the base of the Super¬ 
heater, meeting there the current of hot Gases 
from the Generator and being vaporized by 
the heat of the latter passed therewith as vapor 
into the Superheater proper. In the works at 
Worcester the naphtha was forced under pres¬ 
sure through a large coil heated by steam to 
about 350° F., and was then sprayed into the 
base of the Superheater. Except in the par¬ 
ticulars above mentioned, the Gas at both 
places was made under similar conditions and 
from similar materials. 

The samples illustrating the composition of 
the Gas were collected by causing the Gas to 
pass in a rapid current through a series of glass 
tubes, drawn out at each end and connected 


20 


by short pieces of rubber tubing, until the air 
had been expelled, and then sealing each of 
the tubes by melting the ends together with 
the blow-pipe flame. 

The analyses were made in this laboratory, 
chiefly in the apparatus of Prof. Walther Hem- 
pel* for Gas analysis over mercury , although 
some of the more important determinations 
were made by the methods of Bunsen, and in 
the case of duplicates invariably with closely 
accordant results. The photometric tests were 
made with a very exact and complete Bunsen- 
Letheby standard 60 inch photometer, made by 
W. W. Goodwin & Co., of Philadelphia. The 
density determinations were made by means 
of a Bunsen-Schilling diffusion apparatus by 
the same makers. 

I. Composition of the Gas. 

The constituents of all Illuminating Gases 
may be arranged in three classes, namely: 


* Neue methode zur analyse der Case von Dr. Walther Hempel 
—Braunschweig—F. Vieweg u. Sohn, 1880. S. 127. 




21 


1. Heavy hydro-carbons or illuminants 
proper. 

2. Combustible diluents. 

3. Incombustible diluents or impurities. 

The quality of the Gas as a source of light or 

heat is closely dependent upon the nature and 
relative proportions of the individual members 
of the two classes first named. The propor¬ 
tion of the constituents of the third class 
should of course be reduced as far as possible. 

In my study of the composition of the Gran¬ 
ger Gas I have first determined the proportion 
of the heavy hydro-carbons in each sample, 
together with the qualitative nature and pro¬ 
portional amount of the several combustible 
and incombustible diluents, restricting the de¬ 
terminations of the nature and amount of the 
individual heavy hydro-carbons to the com¬ 
plete analysis of the purified holder Gas. 

The results of the analyses were as follows, 
viz.: 

Gas from Generator , Worcester , Mass. 

The composition of the non-luminous Water 
Gas from the Generator of the Granger appa- 


22 


ratus is shown in the following analysis, which 
was made on a sample taken at the commence¬ 
ment of the run. 


Nitrogen. 4.69 

Carbonic Acid. 3.47 

Oxygen. 0.00 

Heavy Hydro-Carbons.... 0.00 

Carbonic Oxide.36.80 

Marsh Gas. 2.16 

Hydrogen.. . 52.88 


100.00 


Gas fro?n Holder. 

WORCESTER. LAKE. 


Nitrogen. 2.64 3.85 

Carbonic Acid. 0.14 0.30 

Oxygen. 0.06 0.01 

Heavy Hydro-Carbons . . . . 12.82 15.43 

Carbonic Oxide.28.26 23.58 

Marsh Gas.18.88 20.95 

Hydrogen.37.20 35-88 


100.00 100.00 


From the foregoing analyses it will be seen 
that the combustible diluents in the Granger 
Gas contain, besides the usual constituents of 
the ordinary non-luminous Water Gas a large 
proportion of Marsh Gas (Methane) and it is 
interesting to note that the ratio of the per¬ 
centage of the heavy hydro-carbons to that of 

















\ 

2 3 

the Marsh Gas is in both the Worcester and 
the Lake samples approximately as 2 : 3. 

Determination of the Character of the Heavy 
Hydro- Carbons. 

In the foregoing analyses I have stated the 
whole amount of the heavy hydro-carbons, 
as such, without entering into the details of the 
character and relative amounts of the different 
hydro-carbons of this class contained in the 
Gas. The specific nature of these must always 
be determined by special tests before the meth¬ 
ods of eudiometric analysis can be applied for 
their quantitative determination. 

The methods of investigation applied for 
the determination of this question were as 
follows: 

1st. Examination of the Tar, 

2d. Examination of the products obtained 
by the action of bromine on the Gas. 

3d. Examination of the products dissolved 
from the Gas on passing the latter through ab¬ 
solute alcohol. 


24 


Examination of the Tar. 

Owing to the small amount of the tar formed 
in the Granger process, great difficulty was ex¬ 
perienced in obtaining sufficient for examina¬ 
tion. A sample of about half a pint of thin 
liquid tar was finally obtained and subjected to 
a fractional distillation. By repeated fraction¬ 
ation a product boiling between 8o° and 85° 
Centigrade and amounting .to 36.32 per cent, 
of the weight of the tar was finally obtained. 
This product was found to consist chiefly of 
Benzole C 6 H 6 . Other products were also ob¬ 
tained corresponding in their boiling points to 
the higher homologues of Benzole. Lack of 
time, however, and the small size of the sample 
prevented a more thorough study of the last- 
named products. But 12 per cent, of the tar 
possessed a higher boiling point than 311. Fah. 

Examination of products obtained by the 
action of Bromine on Water Gas. 

Illuminating Water Gas, prepared as in the 
Granger process by passing a mixture of naph¬ 
tha vapor and non-illuminating Water Gas 


25 


through a hot Superheater, was passed in a slow 
current through Bromine contained in a Pet- 
tenkofer’s tube, until the Bromine had become 
of a light yellowish or brownish color. The 
product was washed with dilute caustic potash 
solution, dried over fused chloride of calcium 
and submitted to fractional distillation. It 
yielded to this treatment 80 per cent, of Bro¬ 
mide of Ethylene, C 2 H 4 Br 2 , a small propor¬ 
tion of Bromide of Methylene (due to the action 
of Bromine on Marsh Gas) and about 12 per 
cent, of a residue that was not volatile without 
decomposition but when heated evolved hydro- 
bromic acid, and on cooling deposited crys¬ 
tals, which, after purification by pressure be¬ 
tween absorbent paper and recrystalization 
from boiling naphtha, yielded a.product con¬ 
sisting of colorless needles and which, on ex¬ 
amination proved to be Tetra-bromide of Naph¬ 
thaline. The pure product thus obtained 
amounted to about 1 per cent, of the weight of 
the mixed Bromides. None of the higher 
members of the Ethylene series (Propylene, 


26 


Butylene, etc.) were present in recognizable 
proportions. 

Examination of products obtamed by solution 
in absolute alcohol. 

A slow current of the dry Gas was allowed to 
pass through absolute alcohol, several weeks be¬ 
ing consumed in the operation. On mixing 
the alcohol with an excess of water a yellowish 
mobile liquid separated, which after being col¬ 
lected, dried over fused calcium chloride and 
subjected to a series of fractional distillations, 
yielded a product boiling between 90° and ioo° 
C., and amounting to about 70 per cent, of the 
weight originally taken. This substance was 
found to consist chiefly of Benzole (C 6 H 6 ). 

The foregoing results show that the heavy hy¬ 
dro-carbons produced by subjecting naphtha 
vapor mixed with non-illuminating Water Gas 
to high temperatures, as in the Granger pro¬ 
cess, consist essentially of Ethylene and Benzole 
vapor, with a small proportion of naphthaline 
vapor, the latter being too insignificent in 


27 

quantity to materially affect the character of 
the Gas. 


In the study of the quantitative proportions 
in which these illuminating hydro-carbons occur 
in the Granger Gas, I have commenced with a 
sample taken from the Condenser at Lake near 
the close of the run, and hence exceptionally 
rich in heavy hydro-carbons. The preliminary 
analysis of this sample shows the composition 
to be: 


Nitrogen,. 4.03 

Carbonic Acid,. 2.66 

Oxygen,. 0.00 

Heavy Hydro-Carbons,.20.36 

Carbonic Oxide, ..17.31 

Marsh Gas,.26.73 

Hydrogen,.28.91 


100.00 


This Gas was subjected to eudiometric analysis 
both before and after removing the heavy hy¬ 
dro-carbons by absorption with fuming sulphuric 
acid. The figures for the contraction by ex¬ 
plosion, volume of Carbonic Acid formed, and 
volume of aqueous vapor, due to the heavy 










28 


hydro-carbons were determined in the usual 

manner by deducting the results of the last- 

named analysis from those of the one -first men¬ 
tioned. 

The data so obtained were as follows: 

Volume of Heavy Hydro-Carbons,.20.36 

Contraction on exploding with Oxygen and Air. . 40 40 

Carbonic Acid formed,. 45-40 

Aqueous Vapor formed.41-92 

These data in connection with the results of 

the qualitative examination above mentioned 

lead to the following figures for the composition 

of the heavy hydrocarbons in question. 

Ethylene,.19.19 vols. 

Benzole Vapor,. 1.17“ 

20.36 vols. 

The theoretical volumes of contraction, Car¬ 
bonic Acid, and Aqueous Vapor, resulting from 
the explosion of a Gas of this composition 
would be: 

Original Volume,.20.36 

Contraction,.41.30 

Carbonic Acid,.45-40 

Aqueous Vapor,.41.89 

The close accordance of these figures with 
those obtained in practice confirm the con¬ 
clusions as to the qualitative nature of the 








2 9 


heavy hydro-carbons based upon the experi¬ 
ments for their isolation and identification 
previously described. 

We have therefore for the composition of 
the Gas in question the following figures: 

Gas fro?n Condenser at Lake . 


Nitrogen,. 4.03 

Carbonic Acid,. 2.66 

Oxygen,. 0.00 

Ethylene,.; . 19.19 

Benzole Vapor,. 1.17 

Carbonic Oxide,.17.31 

Marsh Gas,.26.73 

Hydrogen,.28.91 


100.00 

By similar methods of investigation the com¬ 
position of the Gas from the holders at Wor¬ 
cester and Lake was found to be as follows: 


Gas from Holder . 



Worcester. 

Lake. 

Nitrogen,. 


3-85 

Carbonic Acid, . . . 


0.30 

Oxygen,. 


0.01 

Ethvlene,. 

. . . 11.29 

12.80 

Benzole Vapor, . . . 

• • • 1-53 

2.63 

Carbonic Oxide, . . 


23-58 

Marsh Gas, . . . . 

. . . 18.88 

20.95 

Hydrogen, . . . . 

. . • 37-20 

35-88 


100.00 

100.00 



















3 ° 


For the purpose of comparison I append the 
following analysis of the Coal Gas of the town 
of Heidelberg, Germany, made at the labora¬ 
tory of Bunsen, by Messrs. Kinnicutt and 
Treadwell :* 


Heidelberg Coal Gas. 


Nitrogen,. 2.15 

Carbonic Acid,. 3.01 

Oxygen,. 0.65 

Ethylene,. 2.55 

Propylene,. 1.21 

Benzole Vapor,. 1.33 

Carbonic Oxide,. 8.88 

Marsh Gas,.34-02 

Hydrogen,.46.20 


100.00 


On comparing this analysis of what may be 
accepted as a typical Coal Gas with the Granger 
Gas it will be seen that the latter contains ethy¬ 
lene as the sole representative of the olefiant 
series. In other respects the only difference is 
in the relative proportions of the other con¬ 
stituents contained therein. 


*Gasometrische Methoden, von R. Bunsen, 2te Aufl. S. 142. 












3i 


II. Calorific Value of the Gas. 
i. Calorific equivalent . 

The theoretical calorific equivalent or heat¬ 
ing power of combustibles is the amount of 
heat evolved by the combustion of the unit of 
weight or volume thereof, expressed by the 
number of units of weight of water which can 
thereby be raised in temperature one degree on 
the thermometric scale. 

In this country the units of weight and vol¬ 
ume are respectively the avoirdupois pound 
and the cubic foot, and the measure of temper¬ 
ature the Fahrenheit thermometer. One unit 
of heat therefore, is that quantity of heat which 
will raise the temperature of one pound of 
water one degree on the Fahrenheit scale, and 
n units of heat the amount that would be re¬ 
quired to raise n pounds of water one degree 
Fahrenheit in temperature, or one pound of 
water n degrees. 

In the case of a compound combustible or, 
more properly, a mixture of several combusti- 


3 2 


bles like the Granger Gas, the theoretical calor¬ 
ific equivalent is obtained by multiplying the 
weights of the different constituents, expressed 
in decimals of a pound, by their several calor¬ 
ific equivalents as previously determined by 
experiment. The sum of the numbers so ob¬ 
tained expresses the theoretical calorific equiv¬ 
alent of the mixture. 

The quantity of heat realized by the com¬ 
bustion of the unit of weight of any combus¬ 
tible containing Hydrogen, will vary according 
to whether the water vapor formed during the 
combustion is allowed to escape uncondensed, 
or is condensed to liquid water. In the first 
instance the specific heat of vaporization of 
water must be subtracted from the total amount 
of heat resulting from the combustion. 

The most recent and trustworthy determina¬ 
tions of the heat evolved during the combus¬ 
tion of the several constituents of Illuminating 
Gas are given in the following table: 


33 


Calorific Equivalents of Constituents of 
Illuminating Gas.* 

Heat Units from i lb. 


WATER WATER 
LIQUID. VAPOR. 

Ethylene,.21524.4 20134.8 

Propylene,.21222.0 19834.2 

Benzole Vapor,.18594.0 17847.0 

Carbonic Oxide, .... 4395.6 4395-6 

Marsh Gas,.24021.0 21592.8 

Hydrogen,.61524.0 51804.0 


Proceeding in the manner indicated we ob¬ 
tain the following calorific equivalents: 

Calorific Equivalent of the Granger Gas at 
Worcester, Mass. 


Composition 

IN DECIMALS OF I LB. 

Multipliers. 

Calorific 

Equivalent. 

WATER 

LIQUID 

WATER 

VAPOR 

WATER 

LIQUID 

WATER 

VAPOR 

Nitrogen, . . 

0.04402 

0.0 

0.0 

0.0 

0.0 

Carbonic Acid 

0.00365 

0.0 

0.0 

0.0 

0.0 

Oxygen, . . 

0.00114 

0.0 

0.0 

0.0 

0.0 

Ethylene, . . 

0.18759 

21524.4 

20134.8 

4038.5 

3777-7 

Benzole Vapor, 

0.07077 

18594.0 

17847.0 

1315-8 

1263.0 

Carbonic Oxide 

0.46934 

4395-6 

4395-6 

2063.0 

2063.0 

Marsh Gas, . 

0.17928 

24021.0 

21592.8 

4306.4 

3871.1 

Hydrogen, 

0.04421 

61524.0 

51804.0 

2720.0 

2290.3 


1.00000 



14443-7 

13265.1 


♦Computed from results of J. Thomsen, in A. Naumann’s “ Die 
zie Hungsfrage,” Gissen,i882, S. 61. 


























34 

The total amount of heat evolved on burn¬ 
ing one pound of the Granger Gas at Worces¬ 
ter, Mass., is therefore 14,443.7 units, while if 
the steam produced in the said combustion be 
allowed to escape uncondensed the amount of 
heat will be 13,265.1 units. Under the condi¬ 
tions under which Gas is usually burned for 
heating purposes the latter figure represents the 
calorific equivalent of the Gas: 

The density of the Gas as determined by ex¬ 
periment is 0.5915, whence one cubic foot 
would, at 62° Fahrenheit and 29.92 inch baro¬ 
meter, weigh 0.04501 pounds, avoirdupois, 
hence the calorific value of one cubic foot is as 
follows: 

WATER LIQ. WATER VAP. 

Calorific Equivalent of 

one cubic foot, . . . 650.1 units 597.0 units. 


35 


Calorific Equivalent of Granger Gas, at 
Lake, III. 


Composition 

IN DECIMALS OF I LB. 

Multipliers. 

Calorific 

Equivalent. 

water 

LIQUID. 

WATER 

VAPOR. 

water 

LIQUID. 

WATER 

VAPOR. 

Nitrogen, . . 

0.06175 

0.0 

0.0 

0.0 

0.0 

Carbonic Acid, 

0.00753 

0.0 

0.0 

0.0 

0.0 

Oxygen, . . 

0.00018 

0.0 

0.0 

0.0 

0.0 

Ethylene, . . 

0.20454 

21524.4 

20134.8 

4402.6 

4118.4 

Benzole Vapor 

0.11700 

18594.0 

17847.0 

2175-5 

2088.1 

CarbonicOxide 

0.37664 

4395-6 

4395-6 

1655-6 

I 655-6 

Marsh Gas, . 

0.19133 

24021.0 

21592.8 

4345-9 

4 x 3 r -3 

Hydrogen, 

0.04103 

61524.0 

51804.0 

2524-3 

2125.6 


1.00000 



I 5 I 03-9 

14119.0 


The total amount of heat evolved on burn¬ 
ing one pound of Granger Gas at Lake, Ill., is 
therefore 15,103.9 units, while if the steam 
produced in the combustion be allowed to es¬ 
cape uncondensed the amount of heat will be 
14,119.0 units. 

The density of the Gas being, as determined 
by experiment 0.6018, one cubic foot would 
weigh at 62° Fahrenheit and 29.92 inches baro¬ 
meter 0.04579 tb. whence we have: 

WATER LIQ. WATER VAP. 

Calorific Equivalent of 

one cubic foot . . . 688.7 units. 646.6 units. 





















3 6 

Calorific Equivalent of Coal Gas at 
Heidelberg. 


Composition 

IN DECIMALS OF I LB. 

Multipliers. 

Calorific 

Equivalent. 

water | 
LIQUID. 

WATER 

VAPOR 

WATER 

LIQUID. 

WATER 

VAPOR. 

Nitrogen, . . 

0.04559 

0.0 

0.0 

0.0 

0.0 

Carbonic Acid 

0.09992 

0.0 

0.0 

0.0 

0.0 

Oxygen, . . 

0.01569 

0.0 

0.0 

0.0 

0.0 

Ethylene, . . 

0.05389 

21524.4 

20134.8 

1160.0 

1085.1 

Propylene, 

0.03834 

21222.0 

19834.2 

813.6 

760.4 

Benzole Vapor 

0.07825 

18954.O 

17847.0 

1455.0 

1396.5 

CarbonicOxide 

0.18758 

4395-6 

4395-6 

824.5 

824.5 

Marsh Gas, . 

0.41087 

24021.0 

21592.8 

9869.5 

8871.8 

Hydrogen, 

0.06987 

61524.0 

51804.0 

4298.7 

3619.6 


1.00000 



1 1842I.3 

16557.9 


The total amount of heat evolved on burning 
one pound of this Gas is therefore 18,421.3 
units, while if the steam produced in the com¬ 
bustion be allowed to escape uncondensed the 
amount of heat will be 16,557.9 units. 

The theoretical density of the Gas as calcu¬ 
lated from the analysis is 0.4580, whence at 
62° Fahrenheit and 29.92 inches barometer one 
cubic foot would weigh 0.03485 pounds. 

The calorific equivalent of one cubic foot of 
the Heidelberg Coal Gas is therefore 























37 


WATER LTQ. WATER YAP. 


Calorific Equivalent of 

one cubic foot, . . . 642.0 units. 577-0 units. 

The calorific equivalents of one cubic foot 
of each of the three Gases in question are 
therefore as follows : 

WATER LIQ. WATER VAP. 

Granger Gas, Worcester,.650.1 597-0 

Granger Gas, Lake:.688.7 646.6 

Coal Gas, Heidelberg,.642.0 577 o 

From the foregoing results it will be seen 
that the Granger Gas has a considerably higher 
value as a source of heat than Coal Gas when 
compared by volume. 

2 . Flame- Temperature. 

By the term flame-temperature is understood 
the temperature prevailing in the interior of a 
burning mixture of Gases. The theoretical 
flame-temperature may be computed from the 
calorific equivalents when the specific heats of 
the products of combustion are known. The 
result is very different, according to whether 
the mixture burns under constant pressure or 
with constant volume. When, namely, the 
pressure is constant, and hence the Gas can 





3 « 


expand freely as the temperature rises, a certain 
amount of the heat evolved from the combustion 
is consumed or transformed into mechanical 
energy in performing the work of expansion. 
When, however, the Gas is prevented from ex¬ 
panding during the act of combustion, there 
is no work of expansion to be performed, 
hence the temperature attained by the gaseous 
mixture is higher than in the first instance. 
The increase of flame-temperature caused by 
the use of pressure as in the compound blow, 
pipe or Gas blast, is an illustration of the effects 
of approximating the conditions for combus¬ 
tion with constant volume. 

Under ordinary conditions the flame-tem¬ 
perature under constant pressure, i. e. that of 
the free-burning Gas flame, is the only one with 
which we have to do, and this may be calcu¬ 
lated as follows: 

The calorific equivalent of the unit of weight 
of a mixture of the Gas with just sufficient air 
for its perfect combustion represents the quan¬ 
tity of heat required to raise the unit of weight 
of water so many degrees on the thermomet- 


39 


ric scale, but this heat instead of being con¬ 
sidered as utilized in heating water is here 
utilized solely in heating the gaseous products 
of combustion of this mixture. But much 
less heat is required to raise one pound of Gas 
one degree in temperature than one pound of 
water. Thus, if we call the amount of heat 
required to raise one pound of water one de¬ 
gree Fahrenheit i.ooo, the amounts of heat 
required to raise one pound of Nitrogen, Car¬ 
bonic Acid or Aqueous Vapor one degree will 
be respectively 0.2440, 0.2164 and 0.4750 when 
the Gas is allowed to expand freely on heating, 
and these figures are called the specific heats , 
under constant pressure , of the Gases in question. 

The temperature to which the products of 
combustion of a free-burning mixture of Gases 
may be raised by the heat evolved during this 
combustion, or the “ flame-temperature ,” is 
therefore found by dividing the calorific equiv¬ 
alent of the mixture of combustible Gases and 
air, expressed in heat units , by the specific heat 
of the collective products of combustion of the 


same. 


40 


Proceeding in the manner above indicated, 
we obtain the following figures for the theoret¬ 
ical flame-temperatures of the Gases under con¬ 
sideration. 

Flame-Temperature op the Granger Gas at 
Worcester, Mass . 

At 62° Fah. and 29.92 inches barometer, one 
cubic foot of the Worcester Gas weighs 0.04501 
lbs., requires for its perfect combustion 5.5236 
cubic feet of air and furnishes 6.2040 cubic 
feet of products of combustion, including 
aqueous vapor. The calorific equivalent of 
one pound of the mixture of Air and Gas in 
the above proportions would be as follows : 

COMPOSITION OF COMBUSTIBLE MIX- CALORIFIC 

TURE IN DECIMALS OF I LB. EQUIVALENT. 


Nitrogen, .... 0.69904 X 0.0 = 0.0 

Carbonic Acid, . . 0.00035 X 0 0 = 0.0 

Oxygen,.0.20983 X 0.0 = 0.0 

Ethylene, . . . . 0.0179c X 21 5 2 4-4 = 385.3 

Benzole Vapor, . . 0.00675 X 18594.0 = 125.5 

Carbonic Oxide, . 0.04479 X 4395-6 = 196.9 

Marsh Gas, . . . 0.01712 X 24021.0 = 411.2 

Hydrogen, .... 0.00422 X 61524.0 = 2 59-6 


1.00000 1378.5 

The specific heat of the products of combus¬ 
tion results from the following computation. 








4i 


COMPOSITION OF PRODUCTS OF COM- SPECIFIC 

BUSTION IN DECIMALS OF I LB. HEAT. 


Nitrogen,.0.69904 X 0.2440 = 0.17056 

Carbonic Acid, . . . . 0.19686 X 0 21 64 = 0.04260 
Aqueous Vapor, .... 0.10410 X 0.4750 — 0.04945 


1.00000 0.26261 

Dividing the calorific equivalent by the spe¬ 
cific heat of the products of combustion, we 
have: 

1 37^*5 0-26261 =5249.2° Fah. 

The theoretical elevation of temperature above 
the initial temperature of the gaseous mixture 
is therefore 5249.2 0 Fah. If this initial tem¬ 
perature be 62° Fah. we have as the theoret¬ 
ical flame-temperature of this Gas 

5249.2-I-62 0 = 5311.2 0 Fah. 


Flame-Temperature of the Granger Gas at 
Lake , Illinois. 

At 62° Fah. and 29.92 inches barometer one 
cubic foot of the Lake Gas weighs 0.04579 lbs., 
requires for its perfect combustion 6.1901 cubic 
feet of air and furnishes 6.9060 cubic feet of 
products of combustion, including Aqueous 







42 


Vapor. The calorific equivalent of one pound 
of the combustible mixture is : 

COMPOSITION OF COMBUSTIBLE MIX- CALORIFIC 

TURE IN DECIMALS OF I LB. EQUIVALENT. 


Nitrogen, . . . . 0.70516 X 0.0= 0.0 

Carbonic Acid, . . 0.00067 X 0.0 = 0.0 

Oxygen,.0.21120X 0.0= 0.0 

Ethylene.0.01824 X 21524.4 = 392.6 

Benzole Vapor, . . 0.01043 X 18594.0 = 193-9 

Carbonic Oxide, . 0.03358 X 4395-6 = 147.0 

Marsh Gas, . . .0.01706X24021.0= 409.8 

Hydrogen, .... 0.00366 X 62524.0 = 225.2 


1.00000 1368.5 

The specific heat of the products of combus¬ 
tion is: 

COMPOSITION OF PRODUCTS OF COM- SPECIFIC 

BUSTION IN DECIMALS OF I LB. HEAT. 


Nitrogen,.0.70516 X 0.2440 = 0.17206 

Carbonic Acid, .... 0.19294 X 0.2164 = 0.04175 
Aqueous Vapor, .... 0.10190 X °- 475 ° = 0.04840 


1.00000 0.26221 

Dividing the calorific equivalent of the mix¬ 
ture by the specific heat of the products of 
combustion, we have: 

1368.5 -f- 0.26221 = 5219.i° Fah. 
as the theoretical elevation of temperature 
above the initial temperature of the combus¬ 
tible mixture If the initial temperature be 











43 

62° Fah. we have as the theoretical flame-tem¬ 
perature of this Gas: 

5219.i -f- 62° = 5281.i° Fah. 


Flame- Temperature of Heidelberg Coal Gas. 

From the density calculated from the analy¬ 
sis above cited, viz. : 0.4580, one cubic foot of 
Heidelberg Gas weighs, at 62° Fah. and 29.92 
inches barometer. 0.03485 lbs., requires for its 
complete combustion 5.6298 cubic feet of air 
and furnishes 6.3671 cubic feet of products of 
combustion, including Aqueous Vapor. The 
calorific equivalent of one pound of the com¬ 
bustible mixture is as follows : 

COMPOSITION OF COMBUSTIBLE MIX- CALORIFIC 

TURE IN DECIMALS OF I LB. EQUIVALENT. 


Nitrogen, . . . . 0.7138 X 0.0= 0.0 

Carbonic Acid, . . 0.0075 X 0 0 == o.o 

Oxygen,.0.2156 X 0.0 = 0.0 

Ethylene, . . . . 0.0041 X 2I 5 2 4-4 = 87.4 

Propylene, . . . . 0.0029 X 21222 -° = 61.1 

Benzole Vapor, . . 0.0059 X i 8 594-0 = 109.5 

Carbonic Oxide, . . 0.0141 X 4395-6 = 62.0 

Marsh Gas, .... 0.0309 X 24021.0 = 742.7 

Hydrogen, . . . .0.0052X61524.0= 323.6 


1.0000 1386.3 

The specific heat of the products of combus¬ 
tion is: 









44 


COMPOSITION OF PRODUCTS OF COM- SPECIFIC 

BUSTION IN DECIMALS OF I LB. HEAT. 


Nitrogen,.0.71376 X 0.2440 = 0.17416 

Carbonic Acid, . . . 0.15644 X 0.2164 = 0.03385 
Aqueous Vapor, . . . . 0.12980 X °- 475 ° = 0.06165 


1.00000 0.26966 

Dividing the calorific equivalent by the spe¬ 
cific heat of the products of combustion, we 
have: 


1386.3 ~ 0.26966 = 5140.9 0 Fah. 
as the theoretical elevation of temperature 
above the initial temperature; if the latter be 
62° Fah., we have : 

514 o .9 -f 62= 5202.9 0 Fah. 
as the theoretical flame-temperature of Coal 
Gas. 


The flame-temperatures of the three Gases in 
question are therefore 

Granger Gas, Worcester. . . . 5311.2° Fah. 

Granger Gas, Lake,.. 5281.2° “ 

Coal Gas, Heidelberg,.5202.9 0 “ 

These temperatures all lie beyond the point 
at which dissociation commences, and hence 
would never be attained in practice. Bunsen,* 


*Poggendorff’s Annalen, CXXXI, 171. 









45 


namely, has shown that the percentage of disso¬ 
ciation increases from the point at which it 
commences through the higher temperatures 
being, for instance, in the case of a mixture in 
equivalent proportions of Hydrogen or Carbonic 
Oxide and Oxygen, 50 per cent, at 2000° Centi- 
grade=3632° Fahrenheit, and 66^ per cent, 
at 3000 Centigrade=5432° Fahrenheit. The 
same investigator has also shown that the ex¬ 
treme temperature which may be attained by 
the Oxy-hydrogen blast will not exceed 5432 0 
Fahrenheit. While therefore, the temperatures 
above noted are beyond the limit that may be 
attained in practice the practical results will be 
proportional, in the case of similar gases, to the 
theoretical flame-temperatures, and it may be 
safely assumed that the temperature of the flame 
of the Granger Gas will at least equal and may 
possibly exceed that of the flame of Coal Gas. 

TIL Photometry of the Gas. 

A verage Illuminating Power. 

The results of the photometric tests made at 
Worcester and Lake, on Gas of average charac- 


46 


ter from the holders, using a pressure of y 2 
inch, and corrected for the temperature of 62° 
Fahrenheit, barometric pressure of 30 inches, 
candle consumption of 120 grains of sperma¬ 
ceti per hour, and meter rate of 5 cubic feet 
per hour, were as follows: 


Granger Gas, Worcester,.22.06 Candles. 

Granger Gas, Lake,.26.31 “ 


During my sojourn at Lake I had the oppor¬ 
tunity to convince myself that the candle-power 
of the Gas produced may be regulated at the 
pleasure of the person in charge of the appa¬ 
ratus; the range of candle-power being from 
20 to 29 candles, according to the manipula¬ 
tion employed. 

In the matter of quality the light furnished 
by the Gas both at Lake and at Worcester, was 
of the purest white and yet remarkably soft 
and agreeable to the eye, being in this respect 
greatly superior to Coal Gas. 

Influence of Extreme Cold on Illuminating 
Power . 

The capacity for resisting low temperatures 




47 


is an important requisite for Illuminating Gas 
intended for use in this climate. To test the 
capacity of the Granger Gas in this respect the 
following experiments were tried: 

A length of thirty feet of -inch lead pipe 
was bent into two communicating coils about 
eight inches in diameter. The coils were 
placed in separate tubs and one end of the 
pipe was connected with the service pipe, the 
other end being attached to the photometer 
pipe. The tub next to the photometer was 
filled with water at the temperature of the pho¬ 
tometer room and the Gas turned on. After 
the air had been entirely displaced from the 
pipe and the photometer readings had become 
constant, the candle-power of the Gas was care¬ 
fully determined. The tub adjoining the 
service pipe was then filled with a mixture of 
snow, salt and sal-ammoniac. The Gas was 
allowed to burn at the photometer burner at the 
rate of about five cubic feet per hour until the 
expiration of one hour after the freezing mix¬ 
ture had been applied. The indications of the 
photometer fell gradually from the time of the 


48 


application of the freezing mixture, but were in 
each case stationary for some time previous to the 
final observations of the candle-power. The 
final readings were taken one hour after adding 
the freezing mixture and the temperature of the 
coil noted at the same time. 

For comparison a similar experiment was 
made on the Coal Gas at Worcester, Mass. In 
each case the coils employed were made of 
new lead pipe purchased for that purpose. 

The results of the foregoing experiments 
reduced to standard temperatures and pressures 
etc., are given in the following table: 


Candle 



w 

K 

Power. 


H 

O 


H 



5 w 

ti 

Kind of Gas. 

M 

“ i 

os 5 

«i 

H 5 

ifl B 

0 z 

z 0 

WJ 


(x< 

s o 
w 

H 

0 3 

s§ 

«<S 

h -1 

* 0 

C 0 

u 

hJ < 

0 

w ° 

(X, 

Granger, Worcester, . . 

—7.8 F 

22.06 

17.36 

4.70 

21.30 

Coal Gas, “ . . 

—7.6 F 

18.41 

II -33 

7.08 

38.40 


These figures show that the Granger Gas 
possesses greater power of resistance to the ex¬ 
treme degree of cold employed than Goal Gas 











49 


of much lower candle-power. That this should 
be the case will also appear from a comparison 
of the analyses of the different gases. In the 
Granger Gas the only illuminating ingredient 
susceptible of condensation by cold is the 
Benzole vapor, and in the Worcester Gas this 
constitutes 11.93 percent, of the total illumi¬ 
nating hydro-carbons, while in the Heidelberg 
Gas it constitutes 26.13 P er cent. The illumi¬ 
nating power of Benzole vapor is, however, 
according to Frankland,* when diffused through 
Coal Gas previously deprived of its illuminating 
hydro-carbons by treatment with Bromine, 
nearly six times that of Ethylene similarly em¬ 
ployed. Simple cold will not, of course, con¬ 
dense all of the Benzole vapor from a state of 
admixture with gaseous substances. 

Relations of Chemical Composition to Illumi¬ 
nating Power . 

The luminosity of the flame of Illuminating 
Gas is due to the decomposition by heat of the 
heavy hydro-carbons into lighter hydro-carbons 


*Journalof*the Society of Chemical Industry, III, p. 274. 



50 


and Carbon, the latter being separated in a state 
of extreme subdivision. By the heat of the flame 
this separated Carbon is heated to intense white¬ 
ness and the illuminating effect of the flame is 
due to the light of incandescence of the parti¬ 
cles of Carbon. 

The attainment of the highest degree of 
luminosity of the flame depends upon the 
proper adjustment of the proportion of the 
heavy hydro-carbons (with due regard to their 
individual character), to the nature of the 
diluent mixed therewith. The question of 
the flame temperature of the diluent is here of 
special importance. If the proportion of the 
heavy hydro-carbons be too great in view of 
their density, the heat of combustion will be 
insufficient to raise the whole of the separated 
carbon to a sufficient degree of incandescense 
to permit the attainment of the maximum 
illuminating effect, and the light of that portion 
which is in fact fully incandescent, is, in part, 
intercepted by the less strongly incandescent 
particles. The light emitted will therefore be 
less than should be obtained from the same 


5i 


quantity of heavy hydro carbons burned under 
more suitable conditions. If the excess of 
heavy hydro-carbons be still more marked, in 
proportion to their density, the separated 
Carbon will, in part, escape combustion and 
appear as smoke or lampblack outside of the 
flame. 

It is evident from the foregoing that the 
luminosity of the flame will largely depend 
upon its temperature, for this determines not 
only the decomposition of the heavy hydro¬ 
carbons, but also the degree of incandescence 
of the separated Carbon. The higher the de¬ 
gree of incandescence the purer and whiter 
will be the light furnished from a given pro¬ 
portion of heavy hydro-carbons. Other things 
being equal, the higher the temperature of 
the flame of the combustible diluent the larger 
will be the amount of light furnished by 
a given quantity of heavy hydro-carbons. 
The character of the combustible diluent is 
therefore only second in importance to that of 
the heavy hydro-carbons in its influence on 
the luminosity of the flame. 


52 


But there is yet another condition which has 
a material effect on the degree of luminosity, 
namely, the question whether the combustible 
diluent itself is capable of affording a more or 
less luminous flame. All of the Carbon that 
separates in a flame as such does not remain 
unburned long enough to become incandescent 
and thus add to the luminosity of the flame. 
On the contrary, a certain amount is burned at 
once and has therefore no luminous effect. 
Thus it follows, from the investigations of Percy 
F. Frankland,* that mixtures of Ethylene and 
Hydrogen cease to have any luminous effect when 
the proportion of Ethylene does not exceed ro 
per cent, of the whole Mixtures of Ethylene 
and Carbonic Oxide cease to have any luminous 
effect when the proportion of the former does 
not exceed 20 per cent., while all mixtures of 
Ethylene and Marsh Gas have more or less lumi¬ 
nous effect. The luminosity of a mixture of 
16 per cent. Ethylene and 90 per cent. Marsh 
Gas being equal to about 18 candles, and that 
of one of 20 per cent. Ethylene and 80 per 


* Loc. cit., p. 271, et seq. 



53 


cent. Marsh Gas about 25 candles. The illumi¬ 
nating effect of Marsh Gas alone, when burned 
in an argand burner, is by no means inconsid¬ 
erable,* although this substance has hitherto 
been held to be non-luminous in character. 

As far, therefore, as the object to be obtained 
is the production of the maximum of light 
from the smallest proportion of Ethylene, 
Marsh Gas is unquestionably the best diluent, 
and that this is also true of other hydro-carbons 
than Ethylene is evident from the experiments 
of Frankland and Thorne with Benzole vapor. 
Hence in the case of Coal Gas wherein the 
proportion of Illuminants is restricted by the 
conditions of the manufacture, a large propor¬ 
tion of Marsh Gas is beneficial. On the other 
hand, in the case of Water Gas wherein the 
proportion of Ethylene may be increased at 
pleasure, an excessive proportion of Marsh Gas 
is not only useless, but in the case of Gas of 
high candle power may even prove prejudicial 
on account of the fact that that substance re- 


* L. Wright, Journal of the Chemical Society (English). 1885. 
1 ., 20C-202. 



54 


quires for its combustion a far larger propor¬ 
tion of Oxygen than either Hydrogen or Car¬ 
bonic Oxide, and that the presence of relatively 
large amounts in Gases of high candle power 
increases the danger of imperfect combustion, 
and the attendent evil of a smoky flame, which 
is one of the chief defects of high candle 
power Coal Gas. In the Granger Gas the con¬ 
stituents of the combustible diluent are so pro¬ 
portioned that with the high illuminating effect 
of 26 candles, as in the case of the Lake Gas, 
the flame is of a pure white color, and entirely 
free from tendency to smoke. 

But the highest degree of luminosity from a 
given proportion of illuminants is not the sole 
object to be attained. The amount of heat 
evolved from the flame and the tendency to 
vitiate the air of the rooms in which the gas is 
burned, must also be taken into account in the 
case of Gas intended for illuminating purposes. 
Marsh Gas consumes four times as much 
Oxygen as the same volume of Hydrogen, pro¬ 
duces three times as much heat and furnishes 
its own volume of Carbonic Acid. 


55 


Of the incombustible diluents, Carbonic Acid 
is the most prejudicial. Nitrogen acts only by 
reason of its specific heat in lowering the tem¬ 
perature of the flame and is a much less objec¬ 
tionable impurity than Carbonic Acid. 

IV. Density of the Gas. 

In the following table are given the densi¬ 
ties obtained by experiment in the cases of the 
Granger Gas at Worcester and Lake, and for 
comparison, the densities calculated from the 
analyses of these Gases and the Heidelberg 
Coal Gas. 



Density. 


found. 

CALCULATED. 

Worcester, Mass. 

o- 59 i 5 

O.5825 

Lake, Ill. 

0.6018 

O.6057 

Heidelberg Coal Gas . . 

. . . 

O.4580 


The agreement between the theoretical and 
experimental densities in the two first named 
Gases is as close as the processes of deter¬ 
mination would justify us in expecting, and af¬ 
fords a satisfactory confirmation of the correct¬ 
ness of the analytical results previously given. 












V. Purity of the Gas. 


The tests and quantitative determinations 
of impurities in the Granger Gas from the 
holders gave the following results : 

1. Total Sulphur .—The determination of total 
Sulphur in the Gas was made by the London 
Referee’s method. The result showed the Gas 
to contain but 5.11 grains of Sulphur to the 
100 cubic feet. 

2. Sulphuretted Hydrogen .—The Gas was 
free from any appreciable amount of Sulphur¬ 
etted Hydrogen. 

j. Ammonia .— The Ammonia determina¬ 
tion showed the presence of but 0.38 grains to 
the 100 cubic feet of Gas. 

4. Carbonic Acid .—The before-mentioned 
complete analyses of the purified holder Gas 
showed the presence of but 0.14 to 0.30 per 
cent, of Carbonic Acid. 

5. Tar .—The Gas was conducted for 28 hours 
in a moderately rapid current through a glass 
tube loosely packed with pure white jeweler’s 
cotton. At the expiration of the time men- 


57 

tioned the cotton was not discolored nor had 
any appreciable quantity of tarry substances 
condensed thereon. 

The foregoing results show the Gas made in 
the Granger apparatus to be of the highest 
degree of purity and in all respects comparable 
with the best results heretofore attained in the 
technology of Gas making. The London Gas 
Referees, whose requirements are especially 
strict, allow a maximum of 20 grains of Sul¬ 
phur and 5 grains of Ammonia to 100 cubic 
feet. 

Summary of Results. 

The results of the foregoing investigation 
show that the Gas manufactured by the Granger 
process is, as far as concerns the nature of the 
constituents of which it is composed, identical 
with Coal Gas, except in the fact that Ethylene 
is the only representative of the Olefiant series 
present therein. In other respects the Granger 
Gas differs from Coal Gas solely in the relative 
proportion of its various constituents, and it 
is to this difference that the great superiority 
of the Granger Gas over Coal Gas in regard to 


illuminating effect, purity of light, calorific 
power and density is to be ascribed. 

This similarity in composition involves as a 
necessary result, that in its general properties 
the Granger Gas differs from ordinary Coal 
Gas simply as a rich and dense Coal Gas differs 
from one relatively poor and light in char¬ 
acter. 

The analysis of the Holder Gas at Worcester 
and at Lake show a remarkable uniformity in 
composition in the finished product; the dif¬ 
ferences between these two samples being no 
greater in amount or character than those 
which are usually to be found between the 
products furnished by different Coal Gas works 
working on the same variety of coal and using 
the same process of manufacture, while they 
are vastly less than those obtaining between 
works using different varieties of coal and dif¬ 
ferent methods of treatment. Witness the 
enormous variations in composition among the 
various English and Scotch Coal Gases shown 
in Table II, pages 64 and 65. 


59 


This uniformity in composition is an effec¬ 
tive answer to the absurd statements that have 
been made in various quarters that, being a 
mixture of several Gases, Illuminating Water 
Gas must necessarily develop “a tendency 
to stratify in the holder” and that the pro¬ 
duct must vary greatly in composition and 
properties. All Gases diffuse through each 
other as they do in a vacuum and however 
heterogeneous may be the constituents of any 
given mixture of Gases, they become diffused 
to a perfectly uniform mixture in an exceed¬ 
ingly brief interval of time. The samples 
above mentioned were taken from the holders 
while the operation of Gas making was ac¬ 
tively in progress, and the outlet and inlet 
pipes of‘the holder were placed near together, 
so that the gas from the one could readily 
enter the other. The time consumed in taking 
the samples was, in each case longer than the 
duration of a single run, and yet the contents 
of the several sample tubes of the Gas from the 
holder showed no difference in composition. 


6 o 


The same remark applies to the photometric 
tests, which were entirely uniform throughout 
the whole series of observations. 

Concerning the distinctive feature of the 
Granger process, viz. : the employment of me¬ 
chanical pressure to spray the oil at the base of 
the Superheater where it is volatilized by the 
heat of the Gas from the Generator, instead of 
spraying it by a steam jet or introducing it into 
the Generator, I would state as my opinion 
that the Granger process is a very important im¬ 
provement on the systems that have preceded 
it, and especially the processes last named. 

The method of spraying the oil by means of 
a steam jet is objectionable for the reason that, 
at the temperature that prevails in the interior 
of the Superheater, the steam will react upon 
the oil, or, properly speaking, upon the products 
of the action of heat on the oil, and notably on 
the illuminating hydro-carbons of the Gas, with 
the natural result of either reducing the illumi¬ 
nating power or increasing the consumption of 
oil required for the production of Gas of a 
given candle-power. 


6i 


The method of introducing the oil directly 
into the Generator is open to two objections, 
namely : first , that the admixture of the vapor¬ 
ized oil with the Gas is less perfect, whereby 
the danger of irregular and imperfect gasifica¬ 
tion, with the attendant inconveniences of the 
formation of tar and lamp black is increased ; 
and second , that the heat abstracted from the 
Generator for the vaporization and partial gasi¬ 
fication of the oil, tends greatly to reduce the 
temperature of the former and hence to in¬ 
crease the amount of Carbonic Acid produced 
therein. It is, namely, a fact that the question 
whether incandescent coal, when subjected to 
the action of steam, is to furnish Carbonic 
Oxide or Carbonic Acid in admixture with Hy¬ 
drogen is, other things being equal, chiefly one 
of temperature. The lower the temperature the 
larger will be the proportion of Carbonic Acid 
formed. And the formation of any consider¬ 
able proportion of Carbonic Acid is a disadvan¬ 
tage, for the reasons that in the Superheater it 
tends more or less to react upon and destroy 
the heavy hydro-carbons, while what escapes 


62 

this reaction adds to the difficulty and expense 
of purification. 

For purposes of comparison there is given 
in the following table (Table I.) the results of 
the analyses of the Granger Gas from the hold¬ 
ers at Lake and Worcester, together with the 
analysis of the Heidelberg Coal Gas before 
mentioned. 


63 

Table I. 




Granger Gas. 

Coal Gas. 





HEIDEL¬ 



WORCESTER 

LAKE. 

BERG. 

Nitrogen 

• • • • 

2.64 

3-85 

2.15 

Carbonic Acid . . 

O.I4 

0.30 

3 -°i 

Oxygen . 


0.06 

0.01 

0.65 

Ethylene 

.... 

II.29 

12.80 

2.55 

Propylene .... 

0.00 

0.00 

1.21 

Benzole Vapor . . 

i -53 

2.63 

i -33 

Carbonic Oxide . 

28.26 

23-58 

8.88 

Marsh Gas.... 

18.88 

20.95 

34.02 

Hydrogen .... 

37.20 

35-88 

46.20 



100.00 

100.00 

100.00 


Theory, 

0.5825 

0.6057 

0.4580 

Density. 





t 

Practice, 

0.5915 

0.6018 

. . . 

Heat 

Water 




units 

Liquid, 

650.1 

688.7 

642.0 

from 

Water 




i cub. ft. 

Vapor, 

597 -o 

646.6 

577 -o 

Flame-temperature. 

5 , 3 II - 2 °F. 

5281.i°F. 

5202.9°F. 

Av. Candle Power. 

22.06 

26.31 

. . . 

























I 


64 


TABLE 

COMPOSITION OF ENGLISH AND SCOTCH 
HUMPIDGE AND E. 


(Journal of the Society of 


GAS WORKS. 

DATE. 

CARBONIC 

ACID. 

London—City Co.,. 

1851 

0-53 

“ Great Central Co.,. 

a 

0.28 

“ Western Co.,. 

if 

0.13 

“ Imperial Co.. 

ft 

O.29 

“ Chartered Co.,. 

a 

0.00 

“ Imperial Co.,. 

00 

■^4 

ON 

0.00 

“ Chartered Co.,. 

if 

0.00 

“ Houses of Parliamemt,. 

if 

0.00 j. 

“ Gas Light and Coke Co., .... 

1882-84 

0.00 

“ South Metropolitan Co.,. 

a 

0.09 

Redhill, .'. 

a 

0.74 

Gloucester,. 

a 

0.03 

Newcastle-on-Tyne, . 

(( 

0.28 

Brighton,. 

a 

0.03 

Southampton,. 

a 

0.07 

Ipswich,. 

a 

0.06 

Norwich,. 

a 

0.27 

Edinburgh,. 

a 

0.35 

Glasgow,. 

a 

0.29 

St. Andrews,. 

a 

2-73 

Liverpool, . 

tt 

1.70 

Preston. 

a 

0.84 

Nottingham,. 

a 

0.81 

Leeds,. 

tt 

034 

Sheffield. 

a 

0.24 

Birmingham,. 

a 

1.50 

Bristol,. 

a 

0.00 







































65 


II. 

COAL GASES, FROM THE ANALYSES OF 
AND P. F. FRANICLAND. 


Chemical Industry, III, 272-73.) 


NITROGEN. 

OXYGEN. 

HEAVY 

HYDRO¬ 

CARBONS. 

HYDROGEN 

MARSH ‘ 
GAS. 

CARBONIC 

OXIDE. 



3-05 

47.60 

4I.5O 

7-32 

1.80 

O.44 

3-56 

5I.24 

35-28 

7.4O 

I - 5 I 

0-43 

13.06 

25.82 

51.20 

7.85 

5.10 

1.20 

3- 6 7 

4 I-I 5 

40.66 

8.02 

0.38 

0.08 

3-53 

51.81 

35-25 

8-95 

9-73 

I.9I 

4.18 

40.82 

36.57 

6-79 

348 

trace. 

4.41 

50.59 

38.39 

3- r 3 

2.71 

0.00 

8.72 

41.72 

4I.88 

4.98 

5-95 

0.26 

4.41 

47-99 

37-64 

3-75 

3-*9 

0.00 

2.92 

53 -H 

36.55 

4.11 

3-37 

0.49 

4.40 

48.18 

39-41 

3 - 4 i 

2-73 

0.51 

4-95 

48.89 

38.25 

4.64 

5-29 

0.23 

3.62 

50.50 

36.71 

3-37 

2.07 

0.23 

376 

51.62 

38.15 

4 -H 

2-53 

0-39 

3-09 

53-59 

36-74 

3-59 

10.84 

0.12 

4-53 

43.26 

3873 

2.46 

3-03 

0.14 

3.26 

53-79 

36.11 

3-40 

3-64 

1.00 

12.23 

33-24 

42-93 

6.61 

3-°7 

0.06 

10.00 

39 -i 8 

40.26 

7 -H 

2.83 

0.48 

10.04 

36-63 

42.13 

5.16 

6.10 

0.19 

7.90 

36.44 

44.28 

3-39 

4-79 

0.25 

6.22 

43-95 

39-33 

4.62 

2.51 

0.24 

5*63 

45-52 

39.66 

5-63 

4 - 3 2 

0.07 

7.28 

40.23 

42.74 

5.02 

2.56 

0.10 

6.28 

43-05 

43-05 

4.72 

IO.IO 

0.36 

4.76 

40.23 

39.00 

4-05 

5 - 11 

0.27 

4-58 

44-57 

40.70 

4-77 
















































THE 


Granger Water Gas Co., 

Owners of the Patents, 
PHILADELPHIA, PENNA, 



OFFICERS : 

Arthur O. Granger, 

President. 

John G. Reading, 

Vice- President. 
Joseph H. Collins, Jr., 

Secretary and Treasurer. 
George Harding, Attorney. 


DIRECTORS : 

John G. Reading, Philadelphia. 

Henry B. Plant, New York. 

Henry Sanford, “ 

Robert H. Sayre, Bethlehem, Pa. 

Henry C. Butcher, Philadelphia. 
Joseph H. Collins, Jr., “ 
Arthur O. Granger, 


We refer to the following Works under our Improved Process, in operation or now building : 


New Brunswick,.New Jersey. Changed from Lowe Process. 

Jersey City (People’s Co.), “ 

Binghamton,.New York. 

Cohoes,. “ 

Coney Island,. “ Changed from Lowe Process. 

Port Jervis,. “ Changed from Lowe Process. 

Starin’s, Glen Island, . . 

Utica,. “ 

Bloomington,.Illinois. 

Chicago (Consumers' Co.), “ 


Lake (Cook County), . . 


Peoria,. “ 

Quincy,. “ 

Honesdale,.Pennsylvania. Changed from Lowe Process. 

Mauch Chunk,. “ Changed from Lowe Process. 

Wilkes Barre,. “ Changed from Lowe Process. 

York. 

Athol,.Massachusetts. 

Lynn, . . . . *. 

Worcester,. “ 

Marshall,.Michigan. 

Burlington,.Iowa. 

Washington,.D. C. 

Sherbrooke,.Quebec, Changed from Lowe Process. 

St. Hyacinthe,.Quebec. 

Norfolk,.Virginia. Changed from Lowe Process. 


































Our Motto— WATER GAS ON ITS MERITS ! 

Perfection comes with experience. We have built upwards 
of 70 sets of Water Gas Works and our strong points are : 
1st. Economy in materials and labor. 

2d. Simplicity. 

And a new point in Water Gas. 

3d. Freedom from Tar and Lamp Black. 

A. O. Granger & Co., Philadelphia. 


Copyright 1885. 





































































































































































































































































4 

A 

























